CN111232927A - A kind of waste acid recovery method and system - Google Patents
A kind of waste acid recovery method and system Download PDFInfo
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- 239000002253 acid Substances 0.000 title claims abstract description 60
- 239000002699 waste material Substances 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 21
- 238000011084 recovery Methods 0.000 title claims abstract description 16
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 56
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 47
- 239000007788 liquid Substances 0.000 claims abstract description 39
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 28
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 27
- 230000006837 decompression Effects 0.000 claims abstract description 21
- 230000018044 dehydration Effects 0.000 claims abstract description 21
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 21
- 238000001035 drying Methods 0.000 claims abstract description 21
- 239000012528 membrane Substances 0.000 claims abstract description 20
- 239000000919 ceramic Substances 0.000 claims abstract description 17
- 239000000126 substance Substances 0.000 claims abstract description 15
- 239000011780 sodium chloride Substances 0.000 claims abstract description 14
- 239000007787 solid Substances 0.000 claims abstract description 12
- 238000009835 boiling Methods 0.000 claims abstract description 6
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 4
- 229910000403 monosodium phosphate Inorganic materials 0.000 claims abstract description 4
- 235000019799 monosodium phosphate Nutrition 0.000 claims abstract description 4
- 235000002639 sodium chloride Nutrition 0.000 claims abstract description 4
- AJPJDKMHJJGVTQ-UHFFFAOYSA-M sodium dihydrogen phosphate Chemical compound [Na+].OP(O)([O-])=O AJPJDKMHJJGVTQ-UHFFFAOYSA-M 0.000 claims abstract description 4
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 4
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 4
- 239000000084 colloidal system Substances 0.000 claims abstract description 3
- 238000001704 evaporation Methods 0.000 claims description 13
- 238000001914 filtration Methods 0.000 claims description 13
- 229920000742 Cotton Polymers 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 12
- 239000007789 gas Substances 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 4
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 4
- 239000003921 oil Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 2
- 239000012535 impurity Substances 0.000 claims description 2
- 238000010521 absorption reaction Methods 0.000 claims 1
- 238000009833 condensation Methods 0.000 abstract description 7
- 230000005494 condensation Effects 0.000 abstract description 7
- 238000004064 recycling Methods 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 229920002521 macromolecule Polymers 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000003670 easy-to-clean Effects 0.000 description 1
- 238000009713 electroplating Methods 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/30—Alkali metal phosphates
- C01B25/301—Preparation from liquid orthophosphoric acid or from an acid solution or suspension of orthophosphates
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/03—Preparation from chlorides
- C01B7/035—Preparation of hydrogen chloride from chlorides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/06—Preparation of sulfates by double decomposition
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
一种废酸回收方法与系统，将废酸液先收集到废酸液收集池，再经过PP保安过滤器、陶瓷超滤膜除去酸液中的悬浮物、胶体及油质等物质，然后在废酸液中加入氯化钠均匀搅拌，氯化钠溶入废酸液后，泵入减压脱水干燥装置，利用该装置形成的真空条件，使废酸溶液的挥发温度降低，通过加热蒸发，溶液中盐酸以HCL气体形式蒸发出来，再经过冷凝装置，HCL气体用纯水进行吸收并逐渐生成所需浓度的盐酸；废酸液继续蒸发，液态水生成水蒸汽后，经过冷凝装置冷却成液态水回收，剩余物质为硫酸钠、磷酸二氢钠、氯化钠等固态物质。本发明实现了废酸的重复回收利用，利用减压脱水干燥装置降低了废酸的挥发温度，降低了水的沸点，节省了能源消耗。
A waste acid recovery method and system, the waste acid liquid is first collected in a waste acid liquid collection tank, and then the suspended solids, colloids and oily substances in the acid liquid are removed through a PP security filter and a ceramic ultrafiltration membrane, and then Sodium chloride is added to the waste acid solution and stirred evenly. After the sodium chloride is dissolved in the waste acid solution, it is pumped into a decompression dehydration and drying device, and the vacuum condition formed by the device is used to reduce the volatilization temperature of the waste acid solution. The hydrochloric acid in the solution is evaporated in the form of HCL gas, and then passes through the condensation device, and the HCL gas is absorbed by pure water and gradually generates the required concentration of hydrochloric acid; the waste acid liquid continues to evaporate, and the liquid water generates steam, which is cooled to a liquid state through the condensation device The water is recovered, and the remaining substances are solid substances such as sodium sulfate, sodium dihydrogen phosphate, and sodium chloride. The invention realizes the repeated recycling and utilization of waste acid, reduces the volatilization temperature of waste acid, reduces the boiling point of water and saves energy consumption by using a decompression dehydration drying device.
Description
技术领域technical field
本发明涉及化工领域，特别是涉及一种废酸回收方法与系统。The invention relates to the field of chemical industry, in particular to a waste acid recovery method and system.
背景技术Background technique
随着这些年我国对资源的回收利用的重视，同时对工业生产中的危废品的处理更加严格，许多浓液、废液的处理成为了日益严峻的问题，作为工业生产中的废酸液如果直接排放环境，对环境的危害是非常大的，进行综合无害化处理的成本也非常高昂。在线路板行业、电镀生产行业，每天都会产生一部分的浓液、废酸液，其中大多采用综合无害化处理或者委外处理，不但增加了企业的运行成本还造成了资源的浪费。为此，很多企业对生产中的浓液、废液的回收利用工艺研究越来越重视。目前废酸液的处理普遍采用浓缩法、萃取法、结晶法等工艺，但这些工艺有着较为复杂，运行费用高，操作难度较大的缺点。因此，发明一种新的废酸回收工艺替代旧工艺是很有必要的。With the emphasis on resource recycling and utilization in my country in recent years, and the treatment of hazardous wastes in industrial production has become more stringent, the treatment of many concentrated liquids and waste liquids has become an increasingly serious problem. Direct discharge to the environment is very harmful to the environment, and the cost of comprehensive harmless treatment is also very high. In the circuit board industry and electroplating production industry, part of the concentrate and waste acid solution are produced every day, most of which are treated by comprehensive harmless treatment or outsourced treatment, which not only increases the operating cost of the enterprise but also causes waste of resources. For this reason, many enterprises pay more and more attention to the research on the recycling process of concentrated liquid and waste liquid in production. At present, processes such as concentration method, extraction method and crystallization method are generally used for the treatment of waste acid liquid, but these processes have the disadvantages of being relatively complex, high operating cost and difficult to operate. Therefore, it is necessary to invent a new waste acid recovery process to replace the old one.
发明内容SUMMARY OF THE INVENTION
本发明的目的是提供一种废酸回收方法与系统，解决传统的废酸工艺较为复杂，运行费用高和操作难度较大的问题。The purpose of the present invention is to provide a waste acid recovery method and system, which solves the problems that the traditional waste acid process is relatively complicated, the operating cost is high and the operation is difficult.
本发明解决其技术问题所采用的技术方案是：The technical scheme adopted by the present invention to solve its technical problems is:
一种废酸回收方法，其步骤为：A kind of waste acid recovery method, its steps are:
先将废酸液收集池的废酸水泵入PP棉保安过滤器，去除废酸液中的杂质；First, pump the waste acid in the waste acid liquid collection tank into the PP cotton security filter to remove the impurities in the waste acid liquid;
接着利用陶瓷超滤膜池过滤，进一步去除酸液中的悬浮物、胶体及油质；Then use ceramic ultrafiltration membrane tank filtration to further remove suspended solids, colloids and oil in the acid solution;
然后将陶瓷超滤膜池过滤后的废酸液收集到超滤产水池中，并投加固体氯化钠并均匀搅拌，反应生成盐酸溶液；Then the waste acid liquid filtered by the ceramic ultrafiltration membrane tank is collected into the ultrafiltration water production tank, and solid sodium chloride is added and stirred evenly, and the reaction generates a hydrochloric acid solution;
接着将盐酸溶液泵入减压脱水干燥装置，利用减压脱水干燥装置内部形成的真空条件使盐酸溶液的挥发温度降低，同时缓慢加热并搅拌，控制温度低于水的沸点温度，盐酸随之蒸发成氯化氢气体；Then, the hydrochloric acid solution is pumped into the decompression dehydration drying device, and the volatilization temperature of the hydrochloric acid solution is lowered by using the vacuum conditions formed inside the decompression dehydration drying device, and at the same time, the temperature is slowly heated and stirred, and the temperature is controlled to be lower than the boiling temperature of water, and the hydrochloric acid evaporates accordingly. into hydrogen chloride gas;
接着将生成的氯化氢气体经冷却后用纯水吸收生成所需浓度的盐酸，通过盐酸收集装置收集；Then the generated hydrogen chloride gas is absorbed with pure water to generate the hydrochloric acid of the required concentration after cooling, and is collected by the hydrochloric acid collection device;
进一步废酸液随着温度的不断升高继续蒸发，液态水沸腾后生成水蒸汽并冷却，通过水收集装置回收液态水；Further, the waste acid liquid continues to evaporate as the temperature continues to rise, and the liquid water is boiled to generate water vapor and cooled, and the liquid water is recovered through the water collection device;
最后随着水蒸汽的不断蒸发，生成硫酸钠、磷酸二氢钠、氯化钠等固态物质，综合回收利用。Finally, with the continuous evaporation of water vapor, solid substances such as sodium sulfate, sodium dihydrogen phosphate, and sodium chloride are generated, which are comprehensively recycled.
进一步地，为了让废酸液与氯化钠能充分反应，在第三个步骤中加入的氯化钠为纯度99％以上的工业氯化钠，加入量为废酸液质量百分比的1～2％，并充分搅拌反应30min。Further, in order to allow the waste acid solution and sodium chloride to fully react, the sodium chloride added in the third step is the industrial sodium chloride with a purity of more than 99%, and the addition is 1 to 2% of the waste acid solution mass percentage. %, and fully stirred the reaction for 30min.
进一步地，为了降低HCL的蒸发温度，以及同时降低后续步骤水的蒸发温度，节约能耗，在第四个步骤中减压脱水干燥装置中的蒸汽压力控制在0.3～0.8MPa，真空压力控制在-90.0～-85.0KPa，蒸发温度控制在40～45℃。Further, in order to reduce the evaporation temperature of HCL, and at the same time reduce the evaporation temperature of water in the subsequent steps, and save energy consumption, in the fourth step, the steam pressure in the decompression dehydration drying device is controlled at 0.3-0.8MPa, and the vacuum pressure is controlled at 0.3-0.8MPa. -90.0～-85.0KPa, the evaporation temperature is controlled at 40～45℃.
本发明还提供一种用于实现上述方法的废酸回收系统，包括废酸液收集池、第一提升泵、PP棉保安过滤器、陶瓷超滤膜池、超滤产水池、第二提升泵、减压脱水干燥装置、第一冷凝装置、盐酸收集装置、第二冷凝装置、水收集装置，所述的废酸液收集池通过第一提升泵连接至PP棉保安过滤器的进口，所述PP棉保安过滤器的出口连接至陶瓷超滤膜池；所述的超滤产水池进口连接至陶瓷超滤膜池，出口通过第二提升泵连接至减压脱水干燥装置；所述的减压脱水干燥装置的其中一个出口连接有第一冷凝装置，所述的第一冷凝装置连接盐酸收集装置；所述的减压脱水干燥装置的另中一个出口连接有第二冷凝装置，所述的第二冷凝装置连接水收集装置。The present invention also provides a waste acid recovery system for realizing the above method, comprising a waste acid liquid collection tank, a first lift pump, a PP cotton security filter, a ceramic ultrafiltration membrane pool, an ultrafiltration water production pool, and a second lift pump , decompression dehydration drying device, first condensing device, hydrochloric acid collecting device, second condensing device, water collecting device, the waste acid liquid collecting tank is connected to the inlet of the PP cotton security filter through the first lifting pump, the The outlet of the PP cotton security filter is connected to the ceramic ultrafiltration membrane tank; the inlet of the ultrafiltration water production tank is connected to the ceramic ultrafiltration membrane tank, and the outlet is connected to the decompression dehydration drying device through the second lift pump; the decompression One of the outlets of the dehydration and drying device is connected with a first condensation device, and the first condensation device is connected with a hydrochloric acid collection device; the other outlet of the decompression dehydration and drying device is connected with a second condensation device, and the first condensation device is connected with a second condensation device. The second condensing device is connected to the water collecting device.
进一步地，为了能更有效地过滤掉废酸液中的一些大颗粒悬浮物质、胶体物质等，所述PP棉保安过滤器的过滤精度为0.1～20微米。Further, in order to more effectively filter out some large particle suspended substances, colloidal substances, etc. in the waste acid solution, the filtration precision of the PP cotton security filter is 0.1-20 microns.
进一步地，为了能更有效地过滤掉废酸液中的悬浮物、大分子、油质等物质，所述陶瓷超滤膜池中超滤膜的过滤精度为0.001～0.02微米。Further, in order to more effectively filter out suspended solids, macromolecules, oil and other substances in the waste acid liquid, the filtration precision of the ultrafiltration membrane in the ceramic ultrafiltration membrane pool is 0.001-0.02 microns.
使用本发明提供的处理方法与系统，实现了废酸的重复回收利用，利用减压脱水干燥装置降低了废酸的挥发温度，降低了水的沸点，节省了能源消耗。Using the treatment method and system provided by the present invention realizes the repeated recycling and utilization of waste acid, reduces the volatilization temperature of waste acid, reduces the boiling point of water, and saves energy consumption by using a decompression dehydration drying device.
附图说明Description of drawings
图1为本发明一种废酸回收方法与系统流程示意图。Fig. 1 is a kind of waste acid recovery method and system flow schematic diagram of the present invention.
具体实施方式Detailed ways
以下将结合附图和实施例，对本发明进行较为详细的说明。The present invention will be described in more detail below with reference to the accompanying drawings and embodiments.
如图1所示的一种废酸回收方法与系统，先将生产车间排放的废酸液(废酸液的主要成分为盐酸、硫酸、磷酸等)在废酸液收集池中收集，再用提升泵泵入PP棉保安过滤器，PP棉保安过滤器采用PP滤芯，具有很好的过滤效率和过滤精度，具有良好的亲水性，能实现油水分离，对水质无污染，耐酸耐碱和有机溶剂，抗腐蚀，过滤阻力小，滤流量大，纳污量大，使用寿命长，工作压力为0.2MPa，工作温度可达80℃。为了能更有效地过滤掉废酸液中的一些大颗粒悬浮物质、胶体物质等，过滤精度优选为0.1～20微米。As shown in Figure 1, a waste acid recovery method and system, first collect the waste acid liquid (the main components of the waste acid liquid are hydrochloric acid, sulfuric acid, phosphoric acid, etc.) discharged from the production workshop in the waste acid liquid collection tank, and then use The lift pump is pumped into the PP cotton security filter. The PP cotton security filter adopts PP filter element, which has good filtration efficiency and filtration accuracy, good hydrophilicity, can achieve oil-water separation, no pollution to water quality, acid and alkali resistance and Organic solvent, anti-corrosion, small filtration resistance, large filtration flow, large dirt holding capacity, long service life, working pressure of 0.2MPa, working temperature up to 80 ℃. In order to more effectively filter out some large particle suspended substances, colloidal substances, etc. in the waste acid solution, the filtering precision is preferably 0.1-20 microns.
接着微滤之后的废酸液进入陶瓷超滤膜池，陶瓷超滤膜具有抗酸碱、耐腐蚀、耐磨、耐有机溶剂的特性，可实现油水分离，化学性能稳定，且易清洗。为了能更有效地利用超滤膜过滤掉废酸液中的悬浮物、大分子、油质等物质，陶瓷超滤膜的过滤精度优选为0.001～0.02微米。Then the waste acid liquid after microfiltration enters the ceramic ultrafiltration membrane tank. The ceramic ultrafiltration membrane has the characteristics of acid and alkali resistance, corrosion resistance, wear resistance and organic solvent resistance, which can realize oil-water separation, stable chemical performance and easy to clean. In order to more effectively use the ultrafiltration membrane to filter out suspended solids, macromolecules, oil and other substances in the waste acid solution, the filtration precision of the ceramic ultrafiltration membrane is preferably 0.001-0.02 microns.
然后将陶瓷超滤膜的产水收集到超滤产水池中，池内安装有液位在线控制装置和机械搅拌装置，并控制搅拌机转速为50r/min；在该池中加入纯度为99％以上的工业氯化钠，加入的量约为废酸液质量百分比的1～2％，充分搅拌均匀反应30min后，用提升泵泵入减压脱水干燥装置。Then, the produced water of the ceramic ultrafiltration membrane is collected into the ultrafiltration water production tank, and the liquid level online control device and the mechanical stirring device are installed in the tank, and the speed of the mixer is controlled to be 50r/min; The amount of industrial sodium chloride added is about 1-2% of the mass percentage of the waste acid solution. After fully stirring and uniformly reacting for 30 minutes, it is pumped into the decompression dehydration drying device with a lift pump.
接着减压脱水干燥装置以蒸汽为加热源，为了降低HCL的蒸发温度，同时降低后续水的蒸发温度，节约能耗，控制蒸汽压力优选为0.3～0.8MPa，并启动减压脱水干燥装置的真空泵，反应釜内呈真空状态，真空压力优选为-90.0～-85.0KPa，废酸液需一边蒸发一边不断搅拌，随着加热温度的不断升高，并控制蒸发温度低于水的沸点温度。优选地，在这一步骤中，控制加热蒸发温度控制在40～45℃，废液中产生的HCL气体不断地挥发出来。Next, the decompression dehydration and drying device uses steam as the heating source. In order to reduce the evaporation temperature of HCL, reduce the evaporation temperature of subsequent water, and save energy, the steam pressure is preferably controlled to be 0.3-0.8MPa, and the vacuum pump of the decompression dehydration and drying device is started. , the reaction kettle is in a vacuum state, the vacuum pressure is preferably -90.0～-85.0KPa, the waste acid liquid needs to be continuously stirred while evaporating, and the evaporation temperature is controlled to be lower than the boiling temperature of water with the continuous increase of the heating temperature. Preferably, in this step, the heating and evaporation temperature is controlled at 40-45° C., and the HCL gas generated in the waste liquid is continuously volatilized.
然后HCL气体经过第一冷凝装置的冷却水进行冷却，在常压状态下HCL气体通入装有纯水的盐酸收集装置(可用盐酸收集桶)中，HCL气体溶入水中生成盐酸液，并随着HCL气体的增加盐酸浓度也不断增加，监测盐酸的浓度，直至达到所需浓度后，切换至另一盐酸收集桶，直至HCL气体被全部吸收，盐酸液可直接回用至生产中。Then, the HCL gas is cooled by the cooling water of the first condensing device. Under normal pressure, the HCL gas is passed into the hydrochloric acid collecting device (the hydrochloric acid collecting bucket can be used) equipped with pure water, and the HCL gas is dissolved in the water to generate hydrochloric acid, which is added with the water. With the increase of HCL gas, the concentration of hydrochloric acid also increases continuously. Monitor the concentration of hydrochloric acid until it reaches the required concentration, and then switch to another hydrochloric acid collection barrel. Until the HCL gas is completely absorbed, the hydrochloric acid solution can be directly reused in production.
当HCL气体挥发完全之后，继续升高蒸发温度直至水的沸点，此时液态水不断形成蒸汽，水蒸汽经过第二冷凝装置的冷却水冷却后，在常压下生成液态水，液态水进入水收集装置中收集。When the HCL gas is completely volatilized, the evaporation temperature continues to increase until the boiling point of water. At this time, the liquid water continuously forms steam. After the water vapor is cooled by the cooling water of the second condensing device, liquid water is formed under normal pressure, and the liquid water enters the water. collected in the collection device.
最后直到减压脱水干燥装置反应釜中的水蒸发完毕，生成硫酸钠、磷酸二氢钠、氯化钠等固态物质，此时停止蒸发，固态物质通过驱动装置排出反应釜，统一收集进行综合回收处理。Finally, until the water in the reaction kettle of the decompression dehydration drying device is evaporated, solid substances such as sodium sulfate, sodium dihydrogen phosphate, and sodium chloride are generated. At this time, the evaporation is stopped, and the solid substances are discharged from the reaction kettle through the driving device. deal with.
本发明中所述的所有装置都可以从市场销售上获得。All devices described in the present invention are commercially available.
上面结合附图对本发明一种废酸回收方法与系统进行了示例性描述，显然本发明具体实现并不受上述方式限制，只要采用了本发明的方法构思和技术方案进行的各种改进，或未经改进直接应用于其它场合的均落在本发明的保护范围之内。A kind of waste acid recovery method and system of the present invention has been exemplarily described above in conjunction with the accompanying drawings. Obviously, the specific implementation of the present invention is not limited by the above-mentioned manner, as long as various improvements carried out by the method concept and technical scheme of the present invention are adopted, or Those that are directly applied to other occasions without modification fall within the protection scope of the present invention.
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